CN104168978A - Process for removing carbon dioxide from a gas stream - Google Patents

Process for removing carbon dioxide from a gas stream Download PDF

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Publication number
CN104168978A
CN104168978A CN201380013274.8A CN201380013274A CN104168978A CN 104168978 A CN104168978 A CN 104168978A CN 201380013274 A CN201380013274 A CN 201380013274A CN 104168978 A CN104168978 A CN 104168978A
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Prior art keywords
adsorbent
carbon dioxide
container
waste gas
industrial waste
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Granted
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CN201380013274.8A
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CN104168978B (en
Inventor
埃尔曼诺·菲利皮
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Casale SA
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Ammonia Casale SA
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0462—Temperature swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/402—Further details for adsorption processes and devices using two beds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/65—Employing advanced heat integration, e.g. Pinch technology
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

Abstract

A process and equipment for removing carbon dioxide from a process gas (G), with a solid adsorbent and temperature swing adsorption, where the carbon dioxide is removed from process gas in either a first bed (B1) or a second bed (B2) of adsorbent, while the other bed is regenerated with heat furnished by the incoming hot process gas; the beds are contained in vessels (V1, V2) with heat exchange tubes or plates (T1, T2), so that the removal of CO2 takes place by contacting the process gas with the bed in the shell side, and regeneration of a bed takes place by passing the hot process gas inside the tubes.

Description

For remove the technique of carbon dioxide from air-flow
Technical field
The present invention relates to a kind of smoke stack emission gas for the flue gas from for example reburner of industrial waste gas or fossil fuel factory and remove the technique of carbon dioxide.The present invention relates to a kind of technique based on Temp .-changing adsorption carbon dioxide on solid absorbent.
Background technology
From the flue gas of combustion process or other oxidizing process, removing carbon dioxide is desirable for environmental problem and/or use carbon dioxide as the raw material of another industrial process.In ammonia and the synthetic field of methyl alcohol, methane or other lighter hydrocarbons, if the reformation of natural gas, LPG (liquefied petroleum gas), naphtha etc. is the common source that ammonia or methane supplement synthesis gas, and need to remove at least part of carbon dioxide in the flue gas that is included in described reforming process.
So-called " wet method " technique comprises uses CO 2-selective solution carrys out detergent industry waste gas.But this has the shortcoming of cleaning solution degraded, for example, generate salt or hazardous compound due to oxidation or with sulphur and reaction of nitrogen oxides.Described cleaning solution needs to change, thereby relates to expense and/or needs and safeguard with removal salt or hazardous compound.
The technology utilization solid absorbent that another is known and operating according to the principle of pressure-variable adsorption (PSA) or Temp .-changing adsorption (TSA).In change by pressure in PSA system and TSA system, CO is controlled in the change of temperature 2catch and release subsequently.The CO that can be preserved by described adsorbent in more detail, 2amount be the function of pressure or temperature.Therefore, captive CO 2can remove by the appropriate change of pressure or temperature in the later stage.From solid absorbent, remove absorbate (as CO 2) be known as the regeneration of adsorbent.In TSA system, absorption usually occurs in compared with regenerating and occur at higher temperature at low temperature.This means that the sorbing material in TSA system needs thermal source for regeneration and conventionally after regeneration, must be cooled.
EP-A-1249264 discloses a kind of for reclaim the technique of carbon dioxide from waste gas, comprise the following steps: make waste gas streams infiltrate semipermeable materials as TSA molecular sieve or active carbon, with the carbon dioxide of relevant portion at least in the method absorption waste gas, and obtain having the permeating airflow of low carbon dioxide content, with desorption carbon dioxide from described semipermeable materials, thereby obtain the air-flow that contains high concentration carbon dioxide.
The present invention is intended to improve the known technology with TSA Adsorption carbon dioxide.Especially, described TSA technique needs the alternating phases of heating and cooling solid absorbent to implement respectively absorption and regeneration (desorption).This can exchange or indirect heat exchange is carried out by direct heat.
Direct heat exchange comprises makes described solid absorbent Direct Contact Heating medium or cooling medium.Directly heating has described heat medium provides the advantage of carrier for desorption carbon dioxide, but same heat medium dilutes described carbon dioxide.Therefore need an additional system from heat medium, to remove CO 2if particularly require pure or substantially pure CO 2.
Indirect heat exchange comprises that described solid catalyst does not contact with heating/cooling medium and keeps separating by heat exchange surface, and for example described heating/cooling medium flows in the tube bank that is embedded in described adsorbent bed.The method is not diluted CO 2but shortcoming is, in the described heating period, it does not provide CO 2the carrier of removing from described bed.In some cases, in order to remove the carbon dioxide of desorption, an additional purge stream is by described bed, but this causes the shortcoming identical with described direct heating process.
Summary of the invention
The invention provides a kind ofly for remove the technique of carbon dioxide from industrial waste gas, and use solid absorbent and Temp .-changing adsorption, by means of at least two solid adsorbent beds or bed group.Described technique is used alternatingly two kinds of operator schemes.In first pattern, described first by with the regeneration of described supplied materials industrial waste gas indirect heat exchange, and described CO then 2in described (previously regeneration) second, be hunted down.Once described second by CO 2institute is saturated, and described technique is switched to the second pattern, now by regenerating described second with the hot industrial waste gas indirect heat exchange of described supplied materials, and then at described first IT carbon dioxide.Described CO absorption 2bed can be cooling continuously in described absorption phase, to remove heat of adsorption, increase the CO that is adsorbed 2amount.
In more detail, the invention discloses a kind of technique, wherein:
-from described industrial waste gas, remove carbon dioxide and alternately occur in first and second of at least described solid absorbent of solid absorbent described at least one, described in the time being included in carbon dioxide in described supplied materials industrial waste gas and being adsorbed in described second, regenerate for first, and vice versa, so that first and second adsorbent alternate load carbon dioxide
-described supplied materials industrial waste gas is by having CO with first or second arbitrary load 2sorbent material indirect heat exchange be cooled, thereby heating and the described load of regenerating have CO 2adsorbent, and
-in the time that described industrial waste gas contacts with another sorbent material, then carbon dioxide is removed from industrial waste gas.
In an especially preferred embodiment, described load has CO 2adsorbent bed remain in the environment of a sealing in described regeneration step.Therefore, load has CO 2the heating of adsorbent occur in an enclosed volume and (wait appearance condition), this means in the time that carbon dioxide is progressively discharged, the pressure in described enclosed volume increases.This preferred embodiment has significant advantage: under pressure, can make described carbon dioxide or carbonated gas use, and this pressure contributes to evacuate described carbon dioxide and do not need carrier or compressor.
More preferably, the carbon dioxide discharging when adsorbent is while leaving described enclosed environment, and the heating that keeps described adsorbent, with the temperature substantially constant of enclosed environment described in keeping in the time that pressure reduces.
According to preferred embodiment, described adsorbent bed is positioned in the shell-side of container separately.The shell-side of container can by close form with extraneous related fittings (as valve) as described in enclosed environment.More preferably, each container comprises that heat exchanger is as pipe or plate in bed as described in being embedded in.Described heat exchanger limits the path separating with outside adsorbent bed.By described gas being supplied to heat exchanger as pipe or industrial waste gas is implemented in the inside of hollow sheeting and load has CO 2adsorbent between indirect heat exchange.
In the time of regenerative process at bed, close arbitrary connector of described shell-side, the carbon dioxide that described shell-side limits an enclosed volume and release thus accumulates under pressure.Once regenerate, can open carbon dioxide under discharge pipe and pressure and leave the shell-side of described bed, and the hot industrial waste gas of pipe or plate side continue to flow when maintaining when pressure drop described in the temperature of adsorbent.Therefore, as d/d CO 2while removal from the shell-side of container, the heating of adsorbent is kept, to work as due to CO 2while leaving container pressure decline, keep the stable of the interior temperature of shell-side.
Alternatively, there iing CO with load 2adsorbent described in after indirect heat exchange, and with for CO 2before the adsorbent contact of the regeneration in advance of removing, described industrial waste gas carries out cooling procedure for the second time.This implements and is generally used for cooling described industrial waste gas to being applicable to CO with additional cooling cooling water or the air of utilizing for the second time 2remove environment temperature or a little more than environment temperature.Preferred described temperature is lower than 50 DEG C and more preferably 20-40 DEG C.This second cooling in, condensed water also can be removed.
Once bed regeneration, described bed is located at high temperature, for example 200 DEG C, and can accept containing CO at it 2before industrial waste gas, be preferably cooled.The cooling of this Regenerative beds can complete by supply cooling medium in aforementioned hot permutoid.Even more preferably, described cooling medium is by means of remove CO in another bed 2the carbon dioxide removal gas flow obtaining in advance.In carbon dioxide absorption, cooling described adsorbent bed is to remove heat of adsorption indirectly.
It should be understood that bed or container any quote group or array, for example parallel (the in parallel) that can be equally applicable to bed or container.Term load has CO 2adsorbent be used for representing described adsorbent, it has caught some CO 2or by CO 2institute is saturated.Term carbon dioxide removal gas represents CO 2industrial waste gas after catching and there is the CO lower than supplied materials gas 2content.In some embodiments and according to carbon dioxide remove degree, described carbon dioxide removal gas substantially for not contain CO 2gas.
Described supplied materials industrial waste gas is generally hot gas and may carrys out spontaneous combustion or oxidizing process, comprises the flue gas of reburner, waste gas, the flue gas in power plant etc. of smelting furnace.Conventionally can be used for CO in the present invention 2remove the gas flow temperature of technique at least 80 DEG C and preferably within the scope of 100-300 DEG C, more preferably 150-250 DEG C.High-temp waste gas or flue gas are conventionally cooling in as recuperation of heat, filtration, pollutant removal etc. in preceding step.Term industrial waste gas in this description can refer to for removing the processed burning gases of carbon dioxide.Described industrial waste gas can be for example flue gas from one-stage converter chimney in ammonia or methanol production factory.
The present invention also aims to a kind of for implementing the equipment of described technique.Described equipment preferably includes at least one first container of removing for carbon dioxide, comprise the first solid adsorption material bed and be embedded in first heat exchanger of described first, the second container that at least one is removed for carbon dioxide, comprises the second solid adsorbent materials bed and is embedded in second heat exchanger of described second.Described heat exchanger limits the inner track of heat exchange medium, and described in each, container has shell-side and heat exchange side, so that directly contact with sorbent material at the mobile medium of shell-side, and separate with sorbent material at the medium on heat exchange side.Described equipment also comprises the device for the selective guiding of supplied materials stream of carbonated industrial waste gas, for following arbitrary in both:
-according to the first path, first wherein said supplied materials industrial waste gas passes into the heat exchange of described the first container, for the sorbent material of regenerating in described the first container, and then passes into the shell-side of described second container, for carrying out the removal of carbon dioxide,
-or according to the second path, first wherein said supplied materials industrial waste gas passes into the heat exchange of described second container, for the sorbent material of regenerating in described second container, and then passes into the shell-side of described the first container, for carrying out the removal of carbon dioxide.
Main advantage of the present invention is described technique continuously-running because the regeneration of first or first group can with industrial waste gas in CO 2in second or second group, be hunted down and occur simultaneously.Another advantage is effective utilization of heat: the hot industrial waste gas of described supplied materials is the thermal source for saturated bed regeneration, in some embodiments simultaneously, the carbon dioxide removal gas that leaves described absorbing process can be used for the bed after cooling regeneration, thereby and reclaims the part heat of described bed.Another advantage as mentioned above, is d/d CO 2available and can in the time there is no carrier as steam or purge gas, be discharged under certain pressure.In addition CO, 2be not diluted and with high-purity for, it is whenever CO 2a significant advantage while being used further.
Advantage of the present invention will illustrate by description preferred and unrestriced embodiment below.
Brief description of the drawings
Fig. 1 is according to preferred embodiment of the invention CO 2remove the block diagram of part.
Fig. 2 and 3 shows the operator scheme of equipment in Fig. 1.
Detailed description of the invention
With reference to Fig. 1, CO 2the critical piece of removing part is the first container V1, second container V2, cooler C and separator S.Container V1 and V2 comprise and are suitable for from gas phase, removing CO by TSA technique 2bed of adsorbent material B1 and B2.Each container V1 and V2 also comprise the heat-exchange tube bundle V1, the V2 that are embedded in described adsorbent bed.
Therefore, described container V1 and V2 have pipe side (pipe is inner) and shell-side (in container and outside pipe).Described shell-side comprises adsorbent bed, and pipe side defines the path of heating or cooling medium.Described shell-side and pipe side are not communicated with at described internal tank.
Pipeline 11,12 is communicated with (namely with pipe T1 internal communication) with the pipe side of described container V1, and pipeline 13,14 is communicated with described shell-side.By similar mode, pipeline 21,22 is communicated with the pipe side of described container V2, and with pipe T2 internal communication, and pipeline 23,24 is communicated with the described shell-side of container V2.
Containing CO 2hot industrial waste gas represent with G.Described supplied materials gas G can guide in the pipe side of described the first container V1 by pipeline 11, or guides to by pipeline 21 in the pipe side of described second container V2.In pipe T1 or T2, mobile industrial waste gas is provided for the heat of adsorbent bed B1 separately or B2 regeneration.TSA principle is followed in regeneration, because the CO of absorption in bed 2amount depend on temperature.Described industrial waste gas is cooled simultaneously, as being cooled to the medium temperature of 60-80 DEG C from the typical inlet temperature of 150-200 DEG C.
The temperature of leaving the industrial waste gas of the pipe of container V1 (or V2) further reduces at described cooler C with in mainly comprising the condensate liquid of water, and W can separate in described separator S.Around under environment temperature, the industrial waste gas that leaves separator S top enters the shell-side of another container V2 (or, respectively, V1), and it contacts to remove CO with adsorbent bed there 2.
In other words, described CO 2in a bed, from industrial waste gas, remove, and the heat that another is providing with identical industrial waste gas regeneration.Therefore described CO 2remove part and there are two operator schemes.Described supplied materials gas G can be imported into pipeline 11 or pipeline 21, and it means the pipe side that imports container V1 or V2.Therefore,, after by one or the other tube bank, described industrial waste gas can or arrive the intake pipeline 15 of described cooler C by pipeline 12 by pipeline 22.The industrial waste gas that leaves separator S top by pipeline 17 can be imported into pipeline 13 or 23, thereby imports the shell-side of V1 or V2.The choice direction of fluid described in some valve (not shown) controls.
Fig. 2 and 3 has illustrated two kinds of relevant operator schemes, the wherein path of gas G in thick line Graphics Processing process.
In Fig. 2, the adsorbent bed B1 of container V1 is by CO 2adsorbent bed B2 saturated and container V2 has prepared to catch CO 2, for example, in previous steps, regenerate.Therefore, described supplied materials industrial waste gas G imports tube bank T1 by pipeline 11, with the described bed B1 that regenerates.Described indirect heat exchange has the described bed of heating for regenerating with refrigerating industry waste gas G to the double dominant of lower temperature for contacting with described bed B2.
As long as described hot industrial waste gas is through pipe T1, B1 bed is by release of carbon dioxide.In this stage, close any part being connected with the shell-side of container V1, as pipeline 13 and 14.Therefore, CO 2pressure in an enclosed volume in release and container V1 increases.Once the regeneration of bed B1 completes, for example, under a certain pressure (1.5bars, if initiation pressure is 1bar), the rich CO in V1 shell-side 2gas is available.Described rich CO 2gas can comprise d/d carbon dioxide and add that some are from previous CO 2catch the residual gas of step.Described pressure is the driving force for reclaiming from described container; Can open pipeline 14 to discharge easily described rich CO 2gas is for further using, and described industrial waste gas continues in pipe side flow until the pressure of shell-side is discharged completely, to maintain the temperature of shell-side, otherwise will reduce together with pressure in processing side temperature, causes at least some CO 2to be adsorbed agent adsorbs again.
Still there is CO 2all the industrial waste gas G of content leave the pipe of container V1 by pipeline 12 and carry out through described cooler C further cooling, preferably for example, to environment temperature or approach environment temperature (30-40 DEG C).Line 18 represents that cooling medium is as air or water, and it does not contact with industrial waste gas.Passing through after separator S (pipeline 16), described cold technology waste gas enters container V2 shell-side by pipeline 23 at once.Here, described industrial waste gas contacts with bed B2, CO 2be adsorbed and obtain carbon dioxide removal gas at pipeline 24 places.
Can be used to the bed B1 of cooling previous regeneration at the described carbon dioxide removal gas at pipeline 24 places.In fact, described has high temperature (as 200 DEG C) after regeneration; With described carbon dioxide removal gas be useful as cooling medium because it has avoided external refrigeration method as the needs of air or water.Certainly, the temperature of carbon dioxide removal gas also will increase; In some cases, described carbon dioxide removal gas can be an additional advantage in the availability of a certain temperature, if for example described gas is introduced into further use.
Once described first B1 regeneration and/or second B2 are saturated, described CO 2remove the pattern that part switches to Fig. 3.In this pattern, described supplied materials gas G is directed in pipe T2 by pipeline 12, i.e. the pipe side of container V2, and leave described pipe by pipeline 22.Then described cooling gas is through subcooler C and separator S, and the shell-side that enters container V1 by pipeline 13 is for contact bed B1 and remove CO 2.The gas of described carbon dioxide removal now at pipeline 14 places out, and CO 2to become callable by means of pipeline 24.
Described in should be appreciated that, illustrate a container V1 and a container V2, but the equivalent embodiments with multiple parallel (in parallel) containers is also rational.In addition, heat exchanger plate or other heat exchangers that tube bank T1 and T2 can be placed in described internal tank replace, as long as their limit a path for heating or cooling medium and shell-side are isolated.

Claims (16)

1. for remove a technique for carbon dioxide from industrial waste gas (G), use solid absorbent and Temp .-changing adsorption, it is characterized in that:
-from described industrial waste gas, remove carbon dioxide alternately to occur in described at least one in first (B1) of solid absorbent and second (B2) of described solid absorbent, described in the time being contained in carbon dioxide in described supplied materials industrial waste gas (G) and being adsorbed in described second, regenerate for first, and vice versa, so that described first and described second sorbent material alternate load carbon dioxide
Be:
-described supplied materials industrial waste gas (G) is by having CO with described first or described second arbitrary load 2adsorbent indirect heat exchange be cooled, thereby heating and the described load of regenerating have CO 2adsorbent,
-in the time that described gas contacts with another adsorbent, CO 2then from the described industrial waste gas being cooled, remove.
2. technique according to claim 1, wherein, when when heating and regenerate with described industrial waste gas indirect heat exchange, described load has CO 2adsorbent bed be maintained in the environment of a sealing so that described load has CO 2the heating of adsorbent occur in a constant volume, and in the time that described carbon dioxide discharges from described adsorbent, the pressure in described enclosed environment increases.
3. technique according to claim 2, the CO wherein discharging when adsorbent 2while leaving described enclosed environment, keep the step of described heating adsorption agent, with the temperature substantially constant of environment described in keeping in the time that pressure reduces.
4. according to the technique described in claim 1-3 any one, wherein CO absorption 2bed be indirectly cooled to remove heat of adsorption, increase the CO being adsorbed 2amount.
5. according to the technique described in aforementioned claim any one, wherein by being passed into, industrial waste gas (G) in the heat exchanger (T1, T2) being embedded in described bed, implements industrial waste gas and load has CO 2adsorbent bed between described indirect heat exchange, described bed is contained in the shell-side of container (V1, V2).
6. technique according to claim 5, wherein when carry out when middle in the regeneration of adsorbent described in the shell-side of container with outside isolated, thereby form an enclosed environment, and the CO being discharged by described adsorbent bed in described shell-side 2under pressure, accumulate.
7. according to the technique described in claim 5 or 6, described heat exchanger is pipe (T1, T2) or hollow sheeting.
8. according to the technique described in aforementioned claim any one, it is characterized in that, described industrial waste gas is owing to having CO with load 2adsorbent described indirect heat exchange and after cooling for the first time, carry out cooling procedure for the second time, and contact and be used for removing CO with adsorbent bed at described industrial waste gas 2remove any condensed water before.
9. according to the technique described in aforementioned claim any one, it is characterized in that, described first or second regenerated respectively after, described bed is by being cooled with cooling medium indirect heat exchange.
10. technique according to claim 9, the Industry Waste air-flow that described cooling medium is carbon dioxide removal.
11. according to the technique described in aforementioned claim any one, and described supplied materials industrial waste gas has the temperature of at least 80 DEG C and preferably in the scope of 100-300 DEG C.
12. techniques according to claim 11, wherein the supplied materials industrial waste gas of 100-300 DEG C has CO in heating and the load of described first or second of regenerating 2adsorbent time be cooled to 60-80 DEG C; Then described gas is by being further cooled to 30-40 DEG C as cooling water or cooling-air heat exchange with suitable cooling medium, and described further cooling gas with another not the adsorbent of load contact.
13. according to the technique described in aforementioned claim any one, and the adsorbent of wherein said not load occurs under the absolute environmental pressure of about 1bar the absorption of carbon dioxide.
14. according to the technique described in aforementioned claim any one, and described industrial waste gas is the gas from hydrocarbon reformation or partial oxidation, as the make-up gas of methyl alcohol or ammonia synthesis.
15. for implementing to remove from air-flow the equipment of carbon dioxide process, and described equipment comprises:
-at least one is for removing first container (V1) of carbon dioxide, first (B1) that it comprises solid adsorbent materials and be embedded in first heat exchanger (T1) of described first,
-at least one is for removing the second container (V2) of carbon dioxide, second (B2) that it comprises solid adsorbent materials and be embedded in second heat exchanger (T2) of described second,
-described heat exchanger is that heat exchange medium limits an inner track, and container thereby there is shell-side and heat exchange side described in each, medium mobile in shell-side directly contacts described sorbent material, and the medium on heat exchange side separates with described sorbent material
-described equipment also comprises the device for the selective guiding of carbonated supplied materials air-flow, for following arbitrary in both:
-according to the first path, first wherein said supplied materials gas pass into the heat exchange (T1) of described the first container, for the sorbent material of regenerating in described the first container, and then passes into the shell-side of described second container, for touching and remove carbon dioxide with described the second bench grafting
-or according to the second path, wherein said supplied materials gas is first by the heat exchange of described second container, be used for the sorbent material of regenerating in described second container, and then pass into the shell-side of described the first container, for touching and remove carbon dioxide with described the first bench grafting.
16. equipment according to claim 14, comprise for when regeneration is while carrying out isolated first or the device of second container shell-side, so that containing CO 2gas described first or the isolated shell-side intrinsic pressure of second container under accumulate, and can open to discharge described containing CO 2the discharger of gas.
CN201380013274.8A 2012-03-13 2013-01-11 For the technique that removing carbon dioxide is removed from air-flow Active CN104168978B (en)

Applications Claiming Priority (3)

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EP12159286.9A EP2638949A1 (en) 2012-03-13 2012-03-13 Process for removing carbon dioxide from a gas stream
EP12159286.9 2012-03-13
PCT/EP2013/050453 WO2013135398A1 (en) 2012-03-13 2013-01-11 Process for removing carbon dioxide from a gas stream

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CN104168978B CN104168978B (en) 2017-06-13

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AU (1) AU2013231676B2 (en)
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